Processes For Converting Oxygenates To Olefins Using Aluminosilicate Catalysts

ABSTRACT

The present invention relates to processes for forming mixed alcohols containing methanol and ethanol. The mixed alcohol can then be used as a feedstock for an oxygenate to olefin reaction system for conversion thereof to ethylene, propylene, and the like. In addition, the olefins produced by the oxygenate to olefin reaction can then be used as monomers for a polymerization of olefin-containing polymers and/or oligomers.

CROSS REFERENCE TO RELATED APPLICATION

This application claims benefit of and priority from U.S. Ser. No. 60/854,832, filed Oct. 27, 2006. The above application is fully incorporated herein by reference.

FIELD OF THE INVENTION

The present invention relates to processes for forming mixed alcohols and processes for forming olefins from mixed alcohols, as well as processes for producing polyolefins therefrom. More particularly, the present invention relates to processes for forming a mixed alcohol feedstock containing at least methanol and varying amounts of ethanol.

BACKGROUND OF THE INVENTION

Light olefins, defined herein as ethylene and propylene and optionally butylene, are important commodity petrochemicals useful in a variety of processes for making plastics and other chemical compounds. Ethylene is used to make various polyethylene plastics, and in making other chemicals vinyl chloride, ethylene oxide, ethyl benzene and alcohol. Propylene is used to make various polypropylene plastics, and in making other chemicals such as acrylonitrile and propylene oxide.

The petrochemical industry has known for some time that oxygenates, especially alcohols, are convertible into light olefins. The preferred conversion process is generally referred to as an oxygenate to olefin (OTO) reaction process. Specifically, in an OTO reaction process, an oxygenate contacts a molecular sieve catalyst composition under conditions effective to convert at least a portion of the oxygenate to light olefins. When methanol is the oxygenate, the process is generally referred to as a methanol to olefin (MTO) reaction process. Methanol is a particularly preferred oxygenate for the synthesis of ethylene and/or propylene.

Methanol is one of the major chemical raw materials, ranking third in volume behind ammonia and ethylene. Worldwide demand for methanol as a chemical raw material continues to rise especially in view of its increasingly important role (along with dimethyl ether) as a source of olefins such as ethylene and propylene and as an alternative energy source, for example, as a motor fuel additive or in the conversion of methanol to gasoline.

Methanol (as well as dimethyl ether) can be produced via the catalytic conversion of a gaseous feedstock comprising hydrogen, carbon monoxide and carbon dioxide. Such a gaseous mixture is commonly referred to as synthesis gas or “syngas”.

Methanol is typically produced from the catalytic reaction of syngas in a methanol synthesis reactor in the presence of a heterogeneous catalyst. For example in one synthesis process, methanol is produced using a copper/zinc catalyst in a water-cooled tubular methanol reactor. In methanol production, syngas undergoes three reactions, only two of which are independent. These reactions are:

CO+2H₂→CH₃OH   (A)

CO₂+3H₂→CH₃OH+H₂O   (B)

H₂O+CO⇄H₂+CO₂   (C)

As can be seen from Reactions B and C, CO₂ can participate in methanol synthesis. Nevertheless, it is desirable to minimize the amount of CO₂ in the syngas for several reasons. In the first place, a low CO₂ content in the syngas results in a more reactive mixture for methanol synthesis provided the CO₂ content is at least about 2%. Furthermore, less CO₂ results in lower consumption of hydrogen and lower production of water. Lower water production is useful in applications where some relative small amounts of water can be present in the methanol product such as, for example, in connection with a methanol to olefins (MTO) process. Production of methanol with low water content thus eliminates the need to distill water from the syngas product methanol.

The syngas stoichiometry for methanol synthesis from syngas is generally described by the following relationship known as the “Stoichiometric Number” or S_(N).

S_(N)=(H₂CO₂)/(CO+CO₂)   (D)

The value of S_(N) theoretically required for methanol synthesis is 2.0. However, for commercial production of methanol from syngas, it is desirable that the value for S_(N) range from about 1.95 to 2.15. Dimethyl ether (DME) may also be produced from syngas using chemistry similar to that used for methanol synthesis.

For example, U.S. Pat. Nos. 6,444,712 and 6,486,219 both describe methods for producing olefins from methanol, by way of using natural gas to make the methanol. The methods include converting the methane component of the natural gas to synthesis gas (syngas) using a steam reformer and a partial oxidation reformer. The syngas from each reformer is combined and sent to a methanol synthesis reactor. The combined syngas stream to the methanol synthesis reactor desirably has a syngas number of from about 1.4 to 2.6. The methanol product is then used as a feed in a methanol to olefin production process.

Autothermal reforming (ATR) involves the addition of air or oxygen with relatively smaller proportions of steam to a hydrocarbon feedstock. Reaction of hydrocarbon with oxygen proceeds according to the following general reaction schemes:

C_(n)H_(m)+(n/2)O₂⇄nCO+(m/2)H₂   (E)

C_(n)H_(m)+(n+m/4)O₂⇄nCO₂+(m/2)H₂O   (F)

When methane is the hydrocarbon undergoing oxidative reforming, these reactions become:

CH₄+½O₂⇄CO+2H₂   (G)

CH₄+2O₂⇄CO₂+2H₂O   (H)

Autothermal reforming employs both steam reforming and oxidative reforming of the hydrocarbon feed. The exothermic oxidation of the feedstock hydrocarbons generates sufficient heat to drive the endothermic steam reforming reaction over the catalyst bed. The ATR procedure is thus run at relatively high temperatures and pressures with a relatively low steam to carbon ratio. The CO₂ content of the syngas from ATR processes, however, is fairly low, as is desirable for methanol synthesis.

Another known reforming process involves primarily partial oxidation of a hydrocarbon feed with an oxygen-containing gas. Catalytic partial oxidation reforming procedures are known; for purposes of this invention, partial oxidation reforming takes place in the absence of a catalyst. Due to the absence of a catalyst, partial oxidation (POX) reforming can operate at very high temperatures with little or no steam addition to the feedstock. Higher pressures than are used in ATR operations can be employed in POX reforming. However, the syngas composition resulting from POX reforming is generally deficient in hydrogen for methanol synthesis, resulting in S_(N) and H₂:CO numbers below 2. On the other hand, the CO₂ content of the resulting syngas is generally very low which is below the optimum value for methanol synthesis.

Much of the methanol made today is made under high purity specifications. Grade A and grade AA methanol are commonly produced. U.S. Pat. No. 4,592,806 discloses a process for producing the grade AA methanol. The grade AA methanol has a maximum ethanol content of 10 ppm and is produced using a distillation column.

As the production of methanol continues to increase, and the new commercial uses of methanol also continue to increase, it would be advantageous to produce variable quality methanol streams, which have particular advantages for specific end uses, and which do not have to meet the stringent requirements of Grades AA and A methanol. It would also be beneficial to provide various processes for which the methanol streams would be of particular benefit.

Additionally, in many MTO reaction processes, the largest component of the oxygenate feedstock is methanol. However, relatively small amounts of oxygenates and/or higher alcohols, such as ethanol, can also be present in the feedstock. Some prior art MTO feedstocks have been treated to reduce the amounts of oxygenates and higher alcohols, while other prior art MTO feedstocks have been augmented to increase their relative content of higher alcohols and other oxygenates, for a variety of reasons. As a result, most prior art MTO processes utilize feedstocks that have undergone multiple processing and/or treatment steps to attain a higher proportion of higher alcohols, with respect to methanol.

In addition, when mixed alcohols are used as feedstocks in OTO reaction processes, water and carbon dioxide formation or retention can cause problems with olefin formation, e.g., reduced conversion efficiency. The prior art has recognized the benefit of reduction of water content and carbon dioxide content in OTO feedstock streams, but has taught complex combinations of process steps, creating increased cost and efficiency problems.

Various patent applications have been directed to compositions comprising catalysts such as SAPOs being used with predominantly methanol-based feedstocks. If any ethanol is used in these systems, it is at a very low level, presumably to prevent the appearance of impurities such as acetaldehyde (e.g., which are formed by selective dehydrogenation of ethanol in the presence of many OTO catalyst compositions) in the olefin-containing product.

The present invention, as described below, details a never before seen combination of OTO process conditions and product formation, which can attain significant improvements over the prior art, including lower levels of impurities such as acetaldehyde.

SUMMARY OF THE INVENTION

One aspect of the invention relates to a process for converting an oxygenate feed to a light olefin product comprising: a) providing the oxygenate feed comprising a majority of methanol and at least about 5 wt % ethanol; b) providing a catalyst composition comprising an aluminosilicate catalyst and a basic metal oxide co-catalyst; and c) contacting the oxygenate feed with the catalyst composition under conditions sufficient to convert at least a portion of the oxygenate feed to a light olefin product.

Another aspect of the invention relates to a process for converting an oxygenate feed to an olefin product comprising: a) providing the oxygenate feed; b) providing a catalyst composition comprising an aluminosilicate catalyst and a basic metal oxide co-catalyst; and c) contacting the oxygenate feed with the catalyst composition under conditions sufficient to convert at least a portion of the oxygenate feed to a light olefin product having (i) a prime olefin ratio of at least 1.5:1, (ii) a prime olefin selectivity of at least 80%, or (iii) both (i) and (ii).

Another aspect of the invention relates to a process for converting an oxygenate feed to an olefin product comprising: a) providing the oxygenate feed comprising a majority of methanol and at least about 5 wt % ethanol; b) providing a catalyst composition comprising an aluminosilicate catalyst; and c) contacting the oxygenate feed with the catalyst composition under conditions sufficient to convert at least a portion of the oxygenate feed to a light olefin product having an aldehyde content of not more than about 3,000 wppm.

When process steps are enumerated by alphanumeric characters herein, it should be understood that their order in the recited process need not be set by the sequential nature of the list, i.e., sequential numbers/letters do not necessarily enumerate sequential steps.

Further, as described herein, it is contemplated that embodiments listed separately, even in different aspects of the invention described herein, may be combined together with one or more other embodiments, provided that the embodiments do not have features that are mutually exclusive.

DETAILED DESCRIPTION OF THE INVENTION A. Introduction

An oxygenate feedstock, particularly a mixed alcohol composition containing methanol and ethanol, is a useful feedstock for a variety of catalytic processes, particularly oxygenate to olefin (OTO) reaction processes, in which a catalyst composition, typically containing a primary oxide catalyst having at least two of Al, Si, and P (e.g., an aluminosilicate molecular sieve, preferably a high-silica aluminosilicate molecular sieve) and preferably a basic metal oxide co-catalyst, can be used to convert the oxygenate feedstock into a light olefin product, e.g., containing ethylene and/or propylene, preferably including ethylene. The olefins can then recovered and used for further processing, e.g., in the manufacture of polyolefins such as polyethylene and/or polypropylene, olefin oligomers, olefin copolymers, mixtures thereof, and/or blends thereof.

In one embodiment, a process for converting an oxygenate feed to a light olefin product comprises: a) providing an oxygenate feed comprising a majority of methanol and at least about 5 wt % ethanol; b) providing a catalyst composition comprising an aluminosilicate catalyst and a basic metal oxide co-catalyst; and c) contacting the oxygenate feed with the catalyst composition under conditions sufficient to convert at least a portion of the oxygenate feed to a light olefin product.

In another embodiment, a process for converting an oxygenate feed to an olefin product comprises: a) providing an oxygenate feed; b) providing a catalyst composition comprising an aluminosilicate catalyst and a basic metal oxide co-catalyst; and c) contacting the oxygenate feed with the catalyst composition under conditions sufficient to convert at least a portion of the oxygenate feed to a light olefin product having (i) a prime olefin ratio of at least 1.5:1, (ii) a prime olefin selectivity of at least 80%, or (iii) both (i) and (ii).

In another embodiment, a process for converting an oxygenate feed to an olefin product comprises: a) providing an oxygenate feed comprising a majority of methanol and at least about 5 wt % ethanol; b) providing a catalyst composition comprising an aluminosilicate catalyst; and c) contacting the oxygenate feed with the catalyst composition under conditions sufficient to convert at least a portion of the oxygenate feed to a light olefin product having an aldehyde content of not more than about 3,000 wppm.

B. Methanol and mixed Alcohol Synthesis Systems

There are numerous technologies available for producing methanol including fermentation or the reaction of synthesis gas (syngas) derived from a hydrocarbon feed stream, which may include natural gas, petroleum liquids, carbonaceous materials including coal, recycled plastics, municipal waste, or any other organic material.

The hydrocarbon feed stream that is used in the conversion of hydrocarbon to syngas is optionally treated to remove impurities that can cause problems in further processing of the hydrocarbon feed stream. These impurities can poison many conventional propylene and ethylene forming catalysts. A majority of the impurities that may be present can be removed in any conventional manner. The hydrocarbon feed is preferably purified to remove sulfur compounds, nitrogen compounds, particulate matter, other condensables, and/or other potential catalyst poisons prior to being converted into syngas.

As mentioned above, the hydrocarbon feed stream may be supplied and/or purified by any conventional means of syngas production, including, for example, autothermal reforming, partial oxidation, steam or CO₂ reforming, or a combination of these chemistries. Methanol and mixed alcohol feedstock compositions and processes for forming same are disclosed, for example, in commonly-owned, co-pending U.S. Provisional Application No. 60/798,383, filed May 8, 2006 and entitled “Process for the Production of Mixed Alcohols”, the disclosure of which is fully incorporated herein by reference.

C. Oxygenate-To-Olefin Conversion Process 1. General Process Description

In one embodiment, the mixed alcohol product composition obtained according to this invention comprises at least a portion of an oxygenate feedstock that is converted to olefin(s) via contact with an olefin forming catalyst to form the olefin product. The olefin product can then be recovered, and water, which generally forms during the conversion of the oxygenate(s) in the mixed alcohol composition to olefins, can advantageously be removed. After removing the water, the olefins can be separated into individual olefin streams, with each individual olefin stream being available for further processing, if desired.

Although the present application specifically describes combining a methanol/ethanol synthesis system with an OTO reaction system, one or more additional components may be included in the feedstock that is directed to the OTO reaction system. For example, the feedstock that is directed to the OTO reaction system optionally contains, in addition to methanol and ethanol, one or more aliphatic-containing compounds such as alcohols, amines, carbonyl compounds for example aldehydes, ketones and carboxylic acids, ethers, halides, mercaptans, sulfides, and the like, and mixtures thereof. The aliphatic moiety of the aliphatic-containing compounds typically contains from 1 to 50 carbon atoms, preferably from 1 to 20 carbon atoms, more preferably from 1 to 10 carbon atoms, most preferably from 1 to 4 carbon atoms.

Non-limiting examples of aliphatic-containing compounds include: alcohols such as methanol, ethanol, n-propanol, isopropanol, and the like, alkyl-mercaptans such as methyl mercaptan and ethyl mercaptan, alkyl-sulfides such as methyl sulfide, alkyl amines such as methyl amine, alkyl ethers such as DME, diethyl ether and methyl ethyl ether, alkyl-halides such as methyl chloride and ethyl chloride, alkyl ketones such as dimethyl ketone, alkyl-aldehydes such as formaldehyde and acetaldehyde, and various organic acids such as formic acid and acetic acid.

The various feedstocks discussed above are converted primarily into one or more olefins. The olefins or olefin monomers produced from the feedstock typically have from 2 to 30 carbon atoms, preferably 2 to 8 carbon atoms, more preferably 2 to 6 carbon atoms, still more preferably 2 to 4 carbons atoms, and most preferably ethylene and/or propylene. Non-limiting examples of olefin monomer(s) include ethylene, propylene, butene-1, pentene-1,4-methyl-pentene-1, hexene-1, octene-1 and decene-1, preferably ethylene, propylene, butene-1, pentene-1,4-methyl-pentene-1, hexene-1, octene-1 and isomers thereof. Other olefin monomers can include, but are not limited to, unsaturated monomers, diolefins having 4 to 18 carbon atoms, conjugated or nonconjugated dienes, polyenes, vinyl monomers, and cyclic olefins.

In a preferred embodiment, the feedstock, which contains methanol and ethanol, can be converted to olefin(s) having 2 to 6 carbons atoms, preferably 2 to 4 carbon atoms, more preferably at least including light olefin(s) (i.e., ethylene and/or propylene), in the presence of a molecular sieve catalyst composition. The most preferred process is generally referred to as an oxygenates-to-olefins (OTO) reaction process. In an OTO process, typically an oxygenated feedstock, most preferably a methanol- and ethanol-containing feedstock, is converted in the presence of a molecular sieve catalyst composition into one or more olefins, preferably and predominantly including ethylene and/or propylene.

In one embodiment, the amount of methanol in the feedstock for the OTO reaction can advantageously be at least about 45 wt %, preferably at least about 50 wt %, for example at least about 60 wt %, at least about 70 wt %, at least about 75 wt %, at least about 80 wt %, at least about 85 wt %, at least about 90 wt %, or at least about 95 wt %, based on the total weight of feedstock and/or the total weight of the oxygenates in the feedstock (including any diluent contained therein). In one embodiment, the amount of methanol in the feedstock for the OTO reaction can preferably be less than about 97 wt %, for example less than about 95 wt %, less than about 90 wt %, less than about 85 wt %, less than about 80 wt %, less than about 75 wt %, or less than about 70 wt %, based on the total weight of feedstock and/or the total weight of the oxygenates in the feedstock (including any diluent contained therein).

In one embodiment, the amount of ethanol in the feedstock for the OTO reaction can advantageously be at least about 3 wt %, preferably at least about 5 wt %, for example at least about 8 wt %, at least about 10 wt %, at least about 12 wt %, at least about 15 wt %, at least about 17 wt %, at least about 20 wt %, or at least about 25 wt %, based on the total weight of feedstock and/or the total weight of the oxygenates in the feedstock (including any diluent contained therein). In one embodiment, the amount of ethanol in the feedstock for the OTO reaction can be less than about 55 wt %, preferably less than 50 wt %, for example less than 45 wt %, less than 40 wt %, less than 35 wt %, less than 30 wt %, less than 25 wt %, less than 20 wt %, less than 15 wt %, or less than 10 wt %, based on the total weight of feedstock and/or the total weight of the oxygenates in the feedstock (including any diluent contained therein).

In one embodiment, the amount of liquid feedstock, fed separately or jointly with a vapor feedstock, to a reactor system can be in the range from about 0.1 wt % to about 85 wt %, preferably from about 1 wt % to about 75 wt %, more preferably from about 5 wt % to about 65 wt %, based on the total weight of the feedstock (including any diluent contained therein). The liquid and vapor feedstocks can be of substantially the same composition, or contain varying proportions of the same or different feedstock components, optionally with the same or different diluent.

2. Description of Olefin Forming Catalyst

Any catalyst capable of converting oxygenates to olefins can be used in this invention. Molecular sieve catalysts are preferred. Examples of such catalysts include zeolite-based, as well as non-zeolite-based, molecular sieves and can be of the large, medium, or small pore type. Molecular sieve materials all have 3-dimensional, four-connected framework structure of corner-sharing [TO₄] tetrahedra, where T can be any tetrahedrally coordinated cation. These molecular sieves are typically described in terms of the size of the ring that defines a pore, where the size is based on the number of T atoms in the ring. Other framework-type characteristics include the arrangement of rings that form a cage, and, when present, the dimension of channels, and the spaces between the cages. See van Bekkum, et al, Introduction to Zeolite Science and Practice, Second Completely Revised and Expanded Edition, Volume 137, pages 1-67, Elsevier Science, B.V., Amsterdam, Netherlands (2001).

Non-limiting examples of molecular sieves include small pore molecular sieves (e.g., AEI, AFT, APC, ATN, ATT, ATV, AWW, BIK, CAS, CHA, CHI, DAC, DDR, EDI, ERI, GOO, KFI, LEV, LOV, LTA, MON, PAU, PHI, RHO, ROG, THO, and substituted forms thereof), medium pore molecular sieves (e.g., AFO, AEL, EUO, HEU, FER, MEL, MFI, MTW, MTT, TON, and substituted forms thereof), large pore molecular sieves (e.g., EMT, FAU, and substituted forms thereof), intergrowths thereof, and combinations thereof. Other molecular sieves include, but are not limited to, ANA, BEA, CFI, CLO, DON, GIS, LTL, MER, MOR, MWW, SOD, intergrowths thereof, and combinations thereof. Non-limiting examples of preferred molecular sieves, particularly for converting an oxygenate-containing feedstock into olefin(s), can include AEL, AFY, AEI, BEA, CHA, EDI, FAU, FER, GIS, LTA, LTL, MER, MFI, MOR, MTT, MWW, TAM, TON, intergrowths thereof, and combinations thereof. In a preferred embodiment, the molecular sieve has an AEI topology and/or a CHA topology (i.e., including an AEI/CHA intergrowth), most preferably at least containing a CHA topology.

The small, medium, and large pore molecular sieves have from a 4-ring to a 12-ring or greater framework-type. In a preferred embodiment, the zeolitic molecular sieves have 6-, 8-, 10-, or 12-ring structures and an average pore size in the range from about 3 Å to 15 Å. In a more preferred embodiment, the molecular sieves, preferably aluminosilicate molecular sieves, have a 6-ring or an 8-ring structure and advantageously an average pore size less than about 5 Å, such as in the range from 3 Å to about 5 Å, for example from 3 Å to about 4.5 Å or from 3.5 Å to about 4.2 Å.

Other non-limiting examples of zeolitic and non-zeolitic molecular sieves include one or a combination of the following: Beta (U.S. Pat. No. 3,308,069), ZSM-5 (U.S. Pat. Nos. 3,702,886, 4,797,267 and 5,783,321), ZSM-11 (U.S. Pat. No. 3,709,979), ZSM-12 (U.S. Pat. No. 3,832,449), ZSM-12 and ZSM-38 (U.S. Pat. No. 3,948,758), ZSM-20, ZSM-22 (U.S. Pat. No. 5,336,478), ZSM-23 (U.S. Pat. No. 4,076,842), ZSM-34 (U.S. Pat. No. 4,086,186), ZSM-35 (U.S. Pat. No. 4,016,245), ZSM-38, ZSM-48 (U.S. Pat. No. 4,397,827), ZSM-50, ZSM-58 (U.S. Pat. No. 4,698,217), MCM-1 (U.S. Pat. No. 4,639,358), MCM-2 (U.S. Pat. No. 4,673,559), MCM-3 (U.S. Pat. No. 4,632,811), MCM-4 (U.S. Pat. No. 4,664,897), MCM-5 (U.S. Pat. No. 4,639,357), MCM-9 (U.S. Pat. No. 4,880,611), MCM-10 (U.S. Pat. No. 4,623,527), MCM-14 (U.S. Pat. No. 4,619,818), MCM-22 (U.S. Pat. No. 4,954,325), MCM-41 (U.S. Pat. No. 5,098,684), M-41S (U.S. Pat. No. 5,102,643), MCM-48 (U.S. Pat. No. 5,198,203), MCM-49 (U.S. Pat. No. 5,236,575), MCM-56 (U.S. Pat. No. 5,362,697), ALPO-11 (U.S. Pat. No. 4,310,440), ultrastable Y zeolite (USY), mordenite, SSZ-13, titanium aluminosilicates (TASOs) such as TASO-45 (European Patent No. EP-A-0 229 295), boron silicates (U.S. Pat. No. 4,254,297), titanium aluminophosphates (TAPOs) (U.S. Pat. No. 4,500,651), mixtures of ZSM-5 and ZSM-11 (U.S. Pat. No. 4,229,424), ECR-18 (U.S. Pat. No. 5,278,345), SAPO-34 bound ALPO-5 (U.S. Pat. No. 5,972,203), those disclosed in International Publication No. WO 98/57743 published Dec. 23, 1988 (molecular sieve and Fischer-Tropsch), those disclosed in U.S. Pat. No. 6,300,535 (MFI-bound zeolites), mesoporous molecular sieves (U.S. Pat. Nos. 6,284,696, 5,098,684, 5,102,643 and 5,108,725), and the like, and intergrowths and/or combinations thereof. The entire disclosure of each of the references in this paragraph is hereby fully incorporated by reference herein.

In a preferred embodiment, the molecular sieve catalyst composition comprises an aluminosilicate catalyst composition, preferably a relatively high-silica aluminosilicate catalyst composition. Relatively high-silica aluminosilicates, as used herein, can advantageously include those having a molar relationship of X₂O₃:(n)YO₂ (wherein X is a trivalent element and Y is a tetravalent element), in which n is at least about 80, preferably at least about 100, for example at least about 120, at least about 150, at least about 180, or at least about 200, and typically not more than about 5000, preferably not more than about 4000, for example not more than about 3500, not more than about 3000, not more than about 2500, or not more than about 2000. Alternatively, n for relatively high-silica aluminosilicates can be from about 300 to about 4000, for example from about 300 to about 2500.

Non-limiting examples of trivalent X can include aluminum, boron, iron, indium, gallium, and combinations thereof, preferably at least including aluminum. Non-limiting examples of tetravalent Y can include silicon, tin, titanium, germanium, and combinations thereof, preferably at least containing silicon.

In embodiments where X represents aluminum and Y represents silicon, the factor n represents a silica:alumina ratio, also termed Si:Al₂. Another measure of relative proportion in such cases is the ratio of Y:X, or the silicon:aluminum ratio. In one embodiment, the silicon:aluminum (Si:Al) ratio of relatively high-silica aluminosilicates is at least about 40, preferably at least about 50, for example at least about 60, at least about 75, at least about 90, or at least about 100, and typically not more than about 2500, preferably not more than about 2000, for example not more than about 1750, not more than about 1500, not more than about 1250, or not more than about 1000. Alternatively, the Si:Al ratio of relatively high-silica aluminosilicates can be from about 150 to about 2000, for example from about 150 to about 1250.

Other non-limiting examples of aluminosilicate catalysts and compositions can be found, for instance, in U.S. Patent Application Publication No. 2003/0176751 and U.S. patent application Ser. Nos. 11/017,286 (filed Dec. 20, 2004) and 60/731,846 (filed Oct. 31, 2005), the disclosures of each of which are incorporated by reference herein.

The catalyst (molecular sieve) used in this invention can include at least in part a chabazite (CHA) framework, an AEI framework, and/or at least one intergrown phase of a CHA framework and an AEI framework. Intergrown molecular sieve phases can be described as disordered planar intergrowths of molecular sieve frameworks, e.g., as referenced in detail in Catalog of Disordered Zeolite Structures, 2000 Edition, published by the Structure Commission of the International Zeolite Association, and in Collection of Simulated XRD Powder Patterns for Zeolites, M. M. J. Treacy and J. B. Higgins, 2001 Edition, published on behalf of the Structure Commission of the International Zeolite Association.

Regular crystalline solids are built from structurally invariant building units, called Periodic Building Units, and are periodically ordered in three dimensions. Structurally disordered structures show periodic ordering in dimensions less than three, i.e. in two, one or zero dimensions. This phenomenon is called stacking disorder of structurally invariant Periodic Building Units. Crystal structures built from Periodic Building Units are called end-member structures if periodic ordering is achieved in all three dimensions. Disordered structures are those where the stacking sequence of the Periodic Building Units deviates from periodic ordering up to statistical stacking sequences.

Analysis of intergrown molecular sieves, such as AEI/CHA intergrowths, can be effected by X-ray diffraction and in particular by comparing the observed patterns with calculated patterns generated using algorithms to simulate the effects of stacking disorder. DIFFaX is a computer program based on a mathematical model for calculating intensities from crystals containing planar faults (see M. M. J. Tracey et al., Proceedings of the Royal Chemical Society, London, A[1991], Vol. 433, pp. 499-520). DIFFaX is the simulation program selected by and available from the International Zeolite Association to simulate the XRD powder patterns for randomly intergrown phases of zeolites (see Collection of Simulated XRD Powder Patterns for Zeolites, by M. M. J. Treacy and J. B. Higgins, 2001, Fourth Edition, published on behalf of the Structure Commission of the International Zeolite Association). It has also been used to theoretically study intergrown phases of AEI, CHA, and KFI, as reported by K. P. Lillerud et al. in Studies in Surface Science and Catalysis, 1994, Vol. 84, pp. 543-550.

Where the crystalline (catalyst) material of the invention comprises a mixture of CHA and AEI or an intergrowth of a CHA framework and an AEI framework, the material can possess a widely varying AEI/CHA ratio of from about 99:1 to about 1:99, such as from about 98:2 to about 2:98, for example from about 95:5 to about 5:95. In one embodiment, where the material is to be used a catalyst in the conversion of oxygenates to olefins, the intergrowth can preferably be CHA-rich and can advantageously have a AEI/CHA ratio ranging from about 5:95 to about 30:70. In addition, in some cases the intergrown material of the invention may comprise a plurality of intergrown phases with a distribution of different AEI/CHA ratios. The relative amounts of AEI and CHA framework-types in the intergrowth can be determined by a variety of known techniques, including, but not limited to, transmission electron microscopy (TEM) and DIFFaX analysis, using the powder X-ray diffraction pattern of a calcined sample of the catalyst.

The catalyst can be incorporated or mixed with other additive materials. Such an admixture is typically referred to as formulated catalyst or as catalyst composition. Preferably, the additive materials are substantially inert to conversion reactions involving dialkyl ethers (e.g., dimethyl ether) and/or alkanols (e.g., methanol, ethanol, and the like).

In one embodiment, one or more other materials can be mixed with the crystalline material, particularly a material that is resistant to the temperatures and other conditions employed in organic conversion processes. Such materials can include catalytically active and inactive materials and synthetic or naturally occurring zeolites, as well as inorganic materials such as clays, silica, and/or other metal oxides such as alumina. The latter may be either naturally occurring or in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides. Use of a catalytically active material can tend to change the conversion and/or selectivity of the catalyst in the oxygenate conversion process. Inactive materials suitably can serve as diluents to control the amount of conversion in the process so that products can be obtained in an economic and orderly manner without employing other means for controlling the rate of reaction. These materials can be incorporated into naturally occurring clays, e.g., bentonite and kaolin, to improve the crush strength of the catalyst under commercial operating conditions. The materials (e.g., clays, oxides, etc.) can function as binders for the catalyst. It can be desirable to provide a catalyst having good crush strength, because, in commercial use, it can be desirable to prevent the catalyst from breaking down into powder-like materials.

Naturally occurring clays that can be employed can include, but are not limited to, the montmorillonite and kaolin family, which families include the subbentonites, and the kaolins commonly known as Dixie, McNamee, Georgia and Florida clays, or others in which the main mineral constituent includes halloysite, kaolinite, dickite, nacrite, or anauxite. Such clays can be used in the raw state as originally mined or initially subjected to calcination, acid treatment, or chemical modification. Other useful binders can include, but are not limited to, inorganic oxides such as silica, titania, beryllia, alumina, and mixtures thereof.

In addition to the foregoing materials, the crystalline material used in this invention can be composited with a porous matrix material such as silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia and silica-titania as well as ternary compositions such as silica-alumina-thoria, silica-alumina-zirconia, silica-alumina-magnesia and silica-magnesia-zirconia.

The relative proportions of crystalline material and inorganic oxide matrix may vary widely. For example, a mixture can include a zeolite content ranging from about 1 to about 90 percent by weight and more usually, particularly when the composite is prepared in the form of beads, in the range from about 2 to about 80 weight percent of the composite.

Additionally or alternately, non-limiting examples of catalyst composition components/materials and/or their relative proportions can be found, e.g., in U.S. Pat. Nos. 5,962,762, 6,004,898, 6,040,264, 6,436,869, 6,448,460, and 6,936,566, inter alia, the disclosures of each of which are fully incorporated herein by reference.

In one embodiment, the catalyst compositions according to the invention can (optionally but preferably) additionally contain an active metal oxide co-catalyst. This metal oxide co-catalyst can be present in many forms and, as follows, in varying degrees of increasing proximity to the molecular sieve catalyst and/or the catalyst composition. For instance, the metal oxide co-catalyst can be present as particulate matter separate from the formulated catalyst composition particles. Additionally or alternately, the metal oxide co-catalyst can be present as a component of the formulated catalyst composition particles. Additionally or alternately, the metal oxide co-catalyst can be coated on the surface and/or in the pores of the molecular sieve catalyst itself.

In one embodiment, active metal oxides are those metal oxides, different from typical binders and/or matrix materials, that, when used in combination with a molecular sieve in a catalyst composition, are effective in extending of the useful life of the catalyst composition. Quantification of the extension in catalyst life is determined by the Lifetime Enhancement Index (LEI) as defined by the following equation:

${L\; E\; I} = \frac{\begin{matrix} {{{Lifetime}\mspace{14mu} {of}\mspace{14mu} {Catalyst}\mspace{14mu} {in}\mspace{14mu} {Combination}}\mspace{14mu}} \\ {{with}\mspace{14mu} {Active}\mspace{14mu} {Metal}\mspace{14mu} {Oxide}} \end{matrix}}{{Lifetime}\mspace{14mu} {of}\mspace{14mu} {Catalyst}}$

where the lifetime of the catalyst or catalyst composition, in the same process under the same conditions, is the cumulative amount of feedstock processed per gram of catalyst composition until the conversion of feedstock by the catalyst composition falls below some defined level, for example 10%. An inactive metal oxide will have little to no effect on the lifetime of the catalyst composition, or will shorten the lifetime of the catalyst composition, and will therefore have a LEI less than or equal to 1. Thus active metal oxides of the invention are those metal oxides, different from typical binders and/or matrix materials, that, when used in combination with a molecular sieve, provide a molecular sieve catalyst composition that has a LEI greater than 1. By definition, a molecular sieve catalyst composition that has not been combined with an active metal oxide will have a LEI equal to 1.0.

It is found that, by including an active metal oxide in combination with a molecular sieve, a catalyst composition can be produced having an LEI from greater than 1 to about 200, for example from about 1.5 to about 100. Typically catalyst compositions according to the invention can exhibit LEI values greater than 1.1, for example from about 1.2 to about 15, and more particularly greater than 1.3, such as greater than 1.5, such as greater than 1.7, such as greater than 2.

In one embodiment, the active metal oxide when combined with a molecular sieve in a catalyst composition enhances the lifetime of the catalyst composition in the conversion of a feedstock comprising methanol, preferably into one or more olefin(s).

In one embodiment in which an active metal oxide co-catalyst is present, the metal oxide co-catalyst is a basic metal oxide. One way of determining basicity in metal oxides involves measuring the absorbance of CO₂ per surface area of metal oxide at a given temperature, e.g., about 100° C. Without being bound by theory, it is postulated that absorbance of CO₂ by the metal oxide indicates the presence of basic sites in the metal oxide and that increasing basicity (or increasing the density of basic sites) of metal oxide typically correlates with increasing CO₂ absorbance. For instance, in some embodiments, the metal oxide co-catalyst can absorb more than 0.03 mg of CO₂ per square meter of metal oxide surface area at about 100° C., for example more than 0.035 mg of CO₂ per square meter of metal oxide surface area at about 100° C., more than 0.04 mg of CO₂ per square meter of metal oxide surface area at about 100° C., more than 0.05 mg of CO₂ per square meter of metal oxide surface area at about 100° C., or more than 0.1 mg of CO₂ per square meter of metal oxide surface area at about 100° C. Alternately or additionally, in some embodiments, the metal oxide co-catalyst can absorb less than 15 mg of CO₂ per square meter of metal oxide surface area at about 100° C., for example less than 10 mg of CO₂ per square meter of metal oxide surface area at about 100° C., less than 7 mg of CO₂ per square meter of metal oxide surface area at about 100° C., less than 5 mg of CO₂ per square meter of metal oxide surface area at about 100° C., or less than 4 mg of CO₂ per square meter of metal oxide surface area at about 100° C.

In order to determine the carbon dioxide uptake of a metal oxide, the following procedure is adopted. A sample of the metal oxide is dehydrated by heating the sample to about 200° C. to 500° C. in flowing air until a constant weight, the “dry weight”, is obtained. The temperature of the sample is then reduced to 100° C. and carbon dioxide is passed over the sample, either continuously or in pulses, again until constant weight is obtained. The increase in weight of the sample in terms of mg/mg of the sample based on the dry weight of the sample is the amount of adsorbed carbon dioxide.

In a preferred embodiment, the carbon dioxide adsorption can be measured using a Mettler TGA/SDTA 851 thermogravimetric analysis system under ambient pressure. Using this apparatus, the metal oxide sample can be dehydrated in flowing air to about 500° C. for one hour. The temperature of the sample can then be reduced in flowing helium to 100° C. After the sample has equilibrated at the desired adsorption temperature in flowing helium, the sample can be subjected to 20 separate pulses (about 12 seconds/pulse) of a gaseous mixture comprising 10 wt % carbon dioxide with the remainder being helium. After each pulse of the adsorbing gas, the metal oxide sample can be flushed with flowing helium for 3 minutes. The increase in weight of the sample, in terms of mg/mg adsorbent, based on the adsorbent weight after treatment at 500° C, typically gives the amount of adsorbed carbon dioxide. The surface area of the sample can be measured in accordance with the method of Brunauer, Emmett, and Teller (BET) published as ASTM D 3663 to provide the carbon dioxide uptake in terms of mg carbon dioxide/m² of the metal oxide.

In one embodiment, the active metal oxide(s) has(have) a BET surface area of greater than 10 m²/g, such as greater than 10 m²/g to about 300 m²/g. In another embodiment, the active metal oxide(s) has a BET surface area greater than 20 m²/g, such as from 20 m²/g to 250 m²/g. In yet another embodiment, the active metal oxide(s) has a BET surface area greater than 25 m²/g, such as from 25 m²/g to about 200 m²/g. In a preferred embodiment, the active metal oxide(s) has a BET surface area greater than 20 m²/g, such as greater than 25 m²/g, and particularly greater than 30 m²/g.

The active metal oxide(s) used herein can be prepared using a variety of methods. It is preferable that the active metal oxide is made from an active metal oxide precursor, such as a metal salt, such as a halide, nitrate, sulfate, or acetate. Other suitable sources of the metal oxide include compounds that form the metal oxide during calcination, such as oxychlorides and nitrates. In one embodiment, the active metal oxide can be made from a hydrated metal oxide precursor. Hydrated metal oxide precursors, such as hydrated zirconia, are disclosed, for example, in U.S. Pat. No. 6,844,291, which is incorporated herein by reference in its entirety. According to one method, the active metal oxide is prepared by the thermal decomposition of metal-containing compounds, such as magnesium oxalate and barium oxalate, at high temperatures, such as 600° C., in flowing air. Thus prepared metal oxides usually have low BET surface area. In another method, the active metal oxide is prepared by the hydrolysis of metal-containing compounds followed by dehydration and calcination. In yet another method, the active metal oxide is prepared by the so-called aerogel method (Koper, O. B., Lagadic, I., Volodin, A. and Klabunde, K. J. Chem. Mater. 1997, 9, 2468-2480). Other aspects of metal oxides and their preparation can be found, e.g., in U.S. Patent Application Publication No. 2003/0171633 A1 and U.S. Pat. No. 6,995,111, the disclosures of each of which are hereby incorporated herein by reference in their entirety.

In one embodiment where hydrated metal oxide precursors are utilized, the hydrated metal oxide precursor can be hydrothermally treated under conditions that include a temperature of at least 80° C., preferably at least 100° C. The hydrothermal treatment typically takes place in a sealed vessel at greater than atmospheric pressure. However, a preferred mode of treatment involves the use of an open vessel under reflux conditions. Agitation of hydrated metal oxides in a liquid medium, for example, by the action of refluxing liquid and/or stirring, can promote the effective interaction of the hydrated oxide with the liquid medium. The duration of the contact of the hydrated oxide with the liquid medium can conveniently be at least 1 hour, such as at least 8 hours. The liquid medium for this treatment typically has a pH of about 6 or greater, such as 8 or greater. Non-limiting examples of suitable liquid media include water, hydroxide solutions (including hydroxides of NH₄ ⁺, Na⁺, K⁺, Mg²⁺, and Ca²⁺), carbonate and bicarbonate solutions (including carbonates and bicarbonates of NH₄ ⁺, Na⁻, K⁺, Mg²⁺, and Ca²⁺), pyridine and its derivatives, and alkyl/hydroxyl amines.

In another embodiment, the active metal oxide is prepared, for example, by subjecting a liquid solution, such as an aqueous solution, comprising a source of ions of a desired metal to conditions sufficient to cause precipitation of a hydrated precursor of the solid oxide material, such as by the addition of a precipitating reagent to the solution. Conveniently, the precipitation can be conducted at a pH above 7. For example, the precipitating agent may be a base such as sodium hydroxide or ammonium hydroxide.

Various methods exist for making mixed metal oxide precursors, e.g., wet impregnation, incipient wetness, and co-precipitation, inter alia.

Non-limiting examples of basic metal oxides include, but are not limited to, hydrotalcite, oxides of metals in Group 2 of the Periodic Table of Elements, oxides of metals in Group 3 of the Periodic Table of Elements, oxides of metals in Group 4 of the Periodic Table of Elements, a mixed metal oxide containing one or more metals of Groups 2, 3, and 4 of the Periodic Table of Elements, or a combination thereof. As used herein, Group 3 metals from the Periodic Table of Elements should be understood to include Lanthanide series metals and Actinide series metals. In one preferred embodiment, the metal oxide co-catalyst comprises an oxide of yttrium. In another preferred embodiment, the metal oxide co-catalyst comprises an oxide of zirconium. In another preferred embodiment, the metal oxide co-catalyst comprises a mixed oxide of yttrium and zirconium. In another preferred embodiment, the metal oxide co-catalyst comprises a mixed oxide of a lanthanide (more preferably, lanthanum) and zirconium. In another preferred embodiment, the metal oxide co-catalyst comprises an oxide of magnesium. In another preferred embodiment, the metal oxide co-catalyst comprises a mixed oxide of a lanthanide (more preferably, lanthanum) and magnesium.

Naturally occurring hydrotalcite is a mineral found in relatively small quantities in a limited number of geographical areas, principally, in Norway and in the Ural Mountains. Natural hydrotalcite has a variable composition depending on the location of the source. Natural hydrotalcite is a hydrated magnesium, aluminum and carbonate-containing composition, which has been found to have the typical composition, represented as Mg₆Al₂(OH)₁₆CO₃.4H₂O. Natural hydrotalcite deposits are generally found intermeshed with spinel and other minerals, such as penninite and muscovite, from which it is difficult to separate the natural hydrotalcite.

Synthetically produced hydrotalcite can be made to have the same composition as natural hydrotalcite, or, because of flexibility in the synthesis, it can be made to have a different composition by replacing the carbonate anion with other anions, such as phosphate ion. In addition, the Mg/Al ratio can be varied to control the basic properties of the hydrotalcite.

A phosphate-modified synthetic hydrotalcite and a process for its synthesis are disclosed in U.S. Pat. No. 4,883,533. U.S. Pat. No. 3,539,306 discloses a process for preparing hydrotalcite which involves mixing an aluminum-containing compound with a magnesium-containing compound in an aqueous medium in the presence of carbonate ion at a pH of at least 8. U.S. Pat. No. 4,656,156 discloses a process for producing synthetic hydrotalcite by heating a magnesium compound to a temperature of about 500 to 900° C. to form activated magnesia, adding the activated magnesia to an aqueous solution containing aluminate, carbonate and hydroxyl ions, and then agitating the resultant mixture at a temperature of about 80 to 100° C. for 20 to 120 minutes to form a low density, high porosity hydrotalcite. A similar process is disclosed in U.S. Pat. No. 4,904,457. The entire disclosure of each of the above references is incorporated herein by reference.

Hydrotalcite compositions containing pillaring organic, inorganic, and mixed organic/inorganic anions are disclosed in U.S. Pat. No. 4,774,212, the entire disclosure of which is incorporated herein by reference. The compositions are anionic magnesium aluminum hydrotalcite clays having large inorganic and/or organic anions located interstitially between positively charged layers of metal hydroxides. The compositions are of the formula:

[Mg_(2x)Al₂(OH)_(4x+4)]Y_(2/n) ^(n−).ZH₂O

where Y is a large organic anion selected from the group consisting of lauryl sulfate, p-toluenesulfonate, terephthalate, 2,5-dihydroxy-1,4-benzenedisulfonate, and 1,5-naphthalenedisulfonate or where Y is an anionic polyoxometalate of vanadium, tungsten or molybdenum. In the above cases, x is from 1.5 to 2.5, n is 1 or 2 and Z is from 0 to 3, except that when Y is polyoxometalate, n is 6.

An aggregated synthetic hydrotalcite having a substantially spheroidal shape and an average spherical diameter of up to about 60 μm, composed of individual platy particles, is disclosed in U.S. Pat. No. 5,364,828, the entire disclosure of which is incorporated herein by reference. This form of hydrotalcite is prepared from aqueous solutions of soluble magnesium and aluminum salts, which are mixed in a molar ratio of from about 2.5:1 to 4:1, together with a basic solution containing at least a two-fold excess of carbonate and a sufficient amount of a base to maintain a pH of the reaction mixture in the range of from about 8.5 to about 9.5.

Prior to use in the catalyst composition of the invention, it may be desirable to calcine the hydrotalcite to remove the water inherently contained by the material. Suitable calcination conditions include a temperature of from about 300° C. to about 800° C., such as from about 400° C. to about 600° C. for about 1 to about 16 hours, such as for about 3 to about 8 hours.

In one embodiment, in which a basic metal oxide co-catalyst is present in combination with the molecular sieve catalyst, the weight/weight ratio of molecular sieve catalyst (alone, without binder, matrix, etc.) to basic metal oxide co-catalyst can be from about 100:1 to about 1:2, preferably from about 50:1 to about 1:1, for example from about 25:1 to about 3:2 or from about 10:1 to about 2:1.

3. Adding Other Oxygenates to Mixed Alcohol Compositions

In an optional embodiment of this invention, the mixed alcohol composition can be converted into olefin(s) along with other oxygenates or diluents. The additional oxygenates or diluents can be co-mixed with the mixed alcohol composition, or can be added as a separate feed stream to an oxygenate conversion reactor in an OTO process. In one embodiment, the additional oxygenate includes one or more alcohols, preferably aliphatic alcohol(s) where the aliphatic moiety of the alcohol(s) has from 3 to 10 carbon atoms, preferably from 3 to 5 carbon atoms, and most preferably from 3 to 4 carbon atoms. The alcohols include lower straight and branched chain aliphatic alcohols and their unsaturated counterparts. Non-limiting examples of additional oxygenates include n-propanol, isopropanol, methyl ethyl ether, dimethyl ether, diethyl ether, diisopropyl ether, methyl propyl ethers, ethyl propyl ethers, methyl butyl ethers such as methyl t-butyl ether, formaldehyde, dimethyl carbonate, dimethyl ketone, acetic acid, and mixtures thereof. In one embodiment, the feedstock for the OTO process can include, aside from methanol and ethanol, one or more of a propanol, dimethyl ether, diethyl ether, methyl t-butyl ether, acetic acid, or a combination thereof.

The mixed alcohol feedstock, in one embodiment, contains one or more diluent(s), typically used to reduce the concentration of alcohol (predominantly methanol), and are generally substantially non-reactive with the oxygenate(s) in the feedstock and/or with the molecular sieve catalyst composition. Non-limiting examples of diluents include helium, argon, nitrogen, carbon monoxide, carbon dioxide, water, essentially non-reactive paraffins (e.g., alkanes such as methane, ethane, propane, and the like), essentially non-reactive aromatic compounds, and mixtures thereof. In one embodiment, the amount of diluent in the feedstock can be from about 0.1 mol % to about 99 mol %, based on the total number of moles of the feedstock and any added diluent, preferably from about 0.5 mol % to about 80 mol %, for example from about 1 mol % to about 50 mol % or from about 3 mol % to about 25 mol %.

4. General Conditions for Converting Methanol/Ethanol to Olefins

According to the OTO reaction process of the invention, oxygenates can be contacted with an olefin forming catalyst to form an olefin product, particularly a light olefin product such as ethylene and/or propylene. The process for converting a feedstock, especially a feedstock containing one or more oxygenates, in the presence of an olefin-forming molecular sieve catalyst composition of the invention, is carried out in a reaction process in a reactor, where the process is a fixed bed process, a fluidized bed process (includes a turbulent bed process), preferably a continuous fluidized bed process, and most preferably a continuous high velocity fluidized bed process.

The OTO reaction processes can take place in a variety of catalytic reactors, for instance, circulating fluidized bed reactors, riser reactors, hybrid reactors that have a dense bed or fixed bed reaction zones and/or fast fluidized bed reaction zones coupled together, and the like. Suitable conventional reactor types can be found, for example, in U.S. Pat. Nos. 4,076,796 and 6,287,522, and in Fluidization Engineering, D. Kunii and O. Levenspiel, Robert E. Krieger Publishing Company, New York, N.Y. (1977), which is herein fully incorporated by reference.

One preferred reactor type is a riser reactor. These types of reactors are generally described, for example, in Riser Reactor, Fluidization and Fluid-Particle Systems, pages 48 to 59, F. A. Zenz and D. F. Othmo, Reinhold Publishing Corporation, New York, 1960, in U.S. Pat. No. 6,166,282 (fast-fluidized bed reactor), and in U.S. patent application Ser. No. 09/564,613 filed May 4, 2000 (multiple riser reactor), which are all herein fully incorporated by reference.

The conversion temperature employed in the conversion process, specifically within the reactor system, is typically from about 392° F. (200° C.) to about 1832° F. (1000° C). In one embodiment, the average reaction temperature employed in the conversion process, specifically within the reactor, can be from about 482° F. (250° C.) to about 1472° F. (800° C.), preferably from about 482° F. (250° C.) to about 1382° F. (750° C.), for example from about 572° F. (300° C.) to about 1202° F. (650° C.), from about 662° F. (350° C.) to about 1112° F. (600° C.), from about 662° F. (350° C.) to about 1022° F. (550° C.), or from about 752° F. (400° C.) to about 932° F. (500° C.).

The pressure employed in the conversion process, specifically within the reactor, is generally not critical. The reaction pressure can desirably be based on the partial pressure of the feedstock, exclusive of any diluent therein. In one embodiment, the reaction pressure employed in the process ranges from about 0.1 kPaa (kPa absolute) to about 5 MPaa (MPa absolute), preferably from about 5 kPaa to about 1 MPaa, most preferably from about 20 kPaa to about 500 kPaa.

The weight hourly space velocity (WHSV), particularly in a process for converting a feedstock containing one or more oxygenates in the presence of a molecular sieve catalyst composition within a reaction zone, is defined as the total weight of the feedstock, excluding any diluents, to the reaction zone per hour per weight of molecular sieve in the molecular sieve catalyst composition in the reaction zone. The WHSV can advantageously be maintained at a level sufficient to keep the catalyst composition in a fluidized state within a reactor.

In one embodiment, the WHSV can range from about 1 hr⁻¹ to about 5000 hr⁻¹, preferably from about 2 hr⁻¹ to about 3000 hr⁻¹, more preferably from about 5 hr⁻¹ to about 1500 hr⁻¹, most preferably from about 10 hr⁻¹ to about 1000 hr⁻¹. In a preferred embodiment, the WHSV can be greater than 20 hr⁻¹. Where a feedstock containing methanol and dimethyl ether is being converted, the WHSV can, in one embodiment, be from about 20 hr⁻¹ to about 300 hr⁻¹.

The superficial gas velocity (SGV) of the feedstock including diluent and reaction products within the reactor system can preferably be sufficient to fluidize the molecular sieve catalyst composition within a reaction zone in the reactor system. In one embodiment, the SGV in the process, particularly within the reactor system, more particularly within the reaction zone of the riser reactor(s), can be at least 0.1 meter per second (m/sec), preferably greater than about 0.5 m/sec, more preferably greater than about 1 m/sec, even more preferably greater than about 2 m/sec, yet even more preferably greater than about 3 m/sec, and most preferably greater than about 4 m/sec. See, for example, U.S. patent application Ser. No. 09/708,753 filed Nov. 8, 2000, the disclosure of which is hereby incorporated by reference.

According to one embodiment, the conversion of oxygenate, particularly the conversion of methanol, to form olefin(s) is from about 90 wt % to about 99.9 wt %. According to another embodiment, the conversion of methanol to olefin(s) is from about 92 wt % to about 99 wt %, typically from about 94 wt % to about 98 wt %.

According to another embodiment, the conversion of methanol to olefin(s) can be above about 98 wt % to less than about 100 wt %. According to another embodiment, the conversion of methanol to olefin(s) can be from about 98.1 wt % to less than about 100 wt %, or alternately from about 98.2 wt % to about 99.8 wt %. According to another embodiment, the conversion of methanol to olefin(s) can be from about 98.2 wt % to less than about 99.5 wt %, or alternately from about 98.2 wt % to about 99 wt %.

It can be desirable to maintain an amount of coke on the catalyst in the reaction vessel, e.g., to enhance the formation of desired olefin product, particularly ethylene and propylene. For instance, in one embodiment, it is particularly desirable that the level of coke on the catalyst in the reactor be at least about 1.5 wt %, preferably from about 2 wt % to about 30 wt %.

5. Impact of Ethylene-Propylene Ratio in OTO Reactions

It has been discovered that ethanol has a selectivity for ethylene under OTO and ETO (ethanol-to-olefins) reaction conditions, which approaches 100 weight percent. Methanol, in contrast, produces ethylene and propylene in generally equal amounts under OTO and ETO reaction conditions. By increasing the amount of ethanol contained in an OTO feedstock, the amount of ethylene produced in the OTO reaction system relative to propylene can be correspondingly increased. See, e.g., U.S. Patent Application Publication No. 2005-0107482, which is incorporated herein by reference in its entirety, for further discussion of ethylene-propylene ratio and its impact on OTO reaction processes, inter alia.

6. OTO Reaction Product Properties and Characteristics

The reaction of oxygenate(s) according to the invention, as facilitated by catalyst compositions according to the invention, inter alia, can advantageously produce an olefin-containing product according to the invention. This olefin-containing product can have various quantifiable properties and characteristics, which can depend on a number of factors including, but not limited to, reaction conditions (e.g., temperatures, pressures, WHSVs, flow rates, etc.), reactor geometry, chemical and/or physical nature of the catalyst composition, catalyst coking levels, catalyst regeneration conditions, oxygenate conversion, oxygenate composition, and the like, and combinations thereof. The aforementioned quantifiable properties and characteristics can include, but are in no way limited to, prime olefin selectivity, prime olefin ratio, impurity content (e.g., aldehydes, acids, alkanes, dienes and/or polyenes, alkynes, ketones, aromatic compounds, alkyl ethers, alkanols, unreacted oxygenates, unreacted syngas/natural gas components, catalyst fines, in some cases α-disubstituted olefins such as isobutylene, in some cases heavier olefins such as C₆+ olefins, and the like, and combinations thereof), and the like.

As used herein, the phrase “prime olefin selectivity” should be understood by one of ordinary skill in the art to mean the conversion-weighted average weight of ethylene and propylene produced in the reaction product divided by the weight of CH₂ groups in the oxygenate feed converted. As used herein, the phrase “prime olefin ratio” should be understood by one of ordinary skill in the art to mean the ratio of the conversion-weighted average yield of ethylene to the conversion-weighted average yield of propylene in the reaction product.

In one embodiment, the prime olefin selectivity (or POS) of the OTO reaction product according to the invention can be greater than 79%, preferably at least 80%, for example from 80% to 95%, from 80% to 90%, or from 80% to 85%, or alternately at least 81%.

In one embodiment, the prime olefin ratio (or POR) of the OTO reaction product according to the invention can be greater than 4:3, more preferably at least 10:7, for example at least 3:2, at least 8:5, at least 13:8, at least 5:3, at least 7:4, at least 9:5, or at least 11:6. In one embodiment, the prime olefin ratio (or POR) of the OTO reaction product according to the invention can be less than 8:3, for example no more than 21:8, no more than 13:5, no more than 5:2, no more than 17:7, no more than 7:3, no more than 9:4, no more than 11:5, or no more than 13:6.

In one embodiment, the amount of aldehyde impurities, particularly the amount of acetaldehyde impurities, in the olefin-containing product can be less than about 10,000 wppm, preferably not more than about 5,000 wppm, for example not more than about 4,000 wppm, not more than about 3,000 wppm, not more than about 2,500 wppm, not more than about 2,000 wppm, not more than about 1,500 wppm, not more than about 1,000 wppm, not more than about 750 wppm, or not more than about 500 wppm, based on the total weight of the feedstock (including any diluent contained therein).

D. Olefin Product Recovery And Use

In one embodiment, olefin product and other gases can be withdrawn from the reactor and passed through a recovery system. Any recovery system, technique, and/or sequence useful in separating olefin(s) and purifying olefin(s) from other gaseous components can be used in this invention. Examples of recovery systems can include, but are not limited to, one or more or a combination of various separation, fractionation, and/or distillation towers, columns, splitters, other associated equipment (e.g. various condensers, heat exchangers, refrigeration systems or chill trains, compressors, knock-out drums or pots, pumps, etc.), and the like, multiples, and combinations thereof.

Non-limiting examples of distillation towers, columns, splitters, or trains used alone or in combination can include one or more of a demethanizer (preferably a high temperature demethanizer), a deethanizer, a depropanizer (preferably a wet depropanizer), a wash tower often referred to as a caustic wash tower and/or quench tower, an absorber, an adsorber, a membrane, an ethylene (C₂) splitter, a propylene (C₃) splitter, a butene (C₄) splitter, and the like, multiples, and combinations thereof.

Various recovery systems useful for recovering predominately olefin(s), preferably prime or light olefin(s) such as ethylene, propylene, and/or butane, are described, for example, in U.S. Pat. Nos. 5,960,643; 5,019,143; 5,452,581; 5,082,481; 5,672,197; 6,069,288; 5,904,880; 5,927,063; 6,121,504; 6,121,503; and 6,293,998; the disclosures of which are all fully incorporated herein by reference.

Generally, accompanying most recovery systems is the production, generation, and/or accumulation of additional products, by-products, and/or contaminants, along with the preferred products [e.g., prime olefin(s)]. The preferred prime products, i.e., light olefins such as ethylene and propylene, are typically purified for use in derivative manufacturing processes, such as polymerization processes. Therefore, in a preferred embodiment of the recovery system, the recovery system also includes a purification system. For example, the light olefin(s) produced, particularly in a MTO process, can be passed through a purification system that removes low levels of by-products and/or contaminants.

Non-limiting examples of contaminants and by-products include generally polar compounds, e.g., water, alcohols, carboxylic acids, ethers, carbon oxides, sulfur compounds (such as hydrogen sulfide, carbonyl sulfides, and mercaptans), ammonia and other nitrogenated compounds, arsine, phosphine, chlorides, and the like, and combinations thereof. Other contaminants and by-products can include, but are not limited to, hydrogen and hydrocarbons such as acetylene, methyl acetylene, propadiene, butadiene, butyne, and the like, and combinations thereof.

Other recovery systems including purification systems, for example for the purification of olefin(s), are described in Kirk-Othmer Encyclopedia of Chemical Technology, 4th Edition, Volume 9, John Wiley & Sons, 1996, pages 249-271 and 894-899, which is hereby incorporated by reference herein. Purification systems are also described in, for example, U.S. Pat. No. 6,271,428, U.S. Pat. No. 6,293,999, and U.S. patent application Ser. No. 09/689,363 filed Oct. 20, 2000, the disclosures of which are hereby incorporated by reference herein.

E. Oligomerization/Polymerization Of Olefin Product

The ethylene and propylene streams produced and recovered according to this invention can be polymerized to form oligomeric, polymeric, and/or plastic compositions, e.g., polyolefins, particularly oligomers, homopolymers, copolymers, and/or blends of monomers, such as ethylene and propylene, formed by a process according to this invention. Any suitable process for forming polyethylene and/or polypropylene oligomers, homopolymers, copolymers, and/or blends can be used. Catalytic polymerization processes are typically preferred. Particularly preferred are metallocene, Ziegler/Natta, aluminum oxide, and acid catalytic systems. See, for example, U.S. Pat. Nos. 3,258,455; 3,305,538; 3,364,190; 5,892,079; 4,659,685; 4,076,698; 3,645,992; 4,302,565; and 4,243,691, the catalyst and process descriptions of each being expressly incorporated herein by reference. In general, these methods involve contacting the ethylene or propylene product with a polyolefin-forming catalyst at a pressure and temperature effective to form the polyolefin product.

In one embodiment, the ethylene or propylene product can be contacted with a metallocene catalyst to form an oligoolefin or a polyolefin (hereinafter, collectively “polyolefin”). In some embodiments, the polyolefin forming process can be carried out at a temperature from about 50° C. to about 320° C., and/or at low, medium, or high pressure, being anywhere from below about 1 barg (1.02 kg/cm² gauge) to about 3200 barg (3264 kg/cm² gauge). For processes desired to be carried out in solution, an inert diluent can be used. In this type of operation, it can be desirable that the pressure range from about 10 barg (10.2 kg/cm² gauge) to about 150 barg (1.53 kg/cm² gauge), and preferably at a temperature from about 120° C. to about 250° C. For gas phase processes, it can be desirable that the temperature generally be from about 60° C. to about 120° C., and that the operating pressure range from about 5 barg (5.1 kg/cm² gauge) to about 50 barg (51 kg/cm² gauge).

In addition to polyolefins, numerous other olefin derivatives may be formed from the olefin products (e.g., ethylene, propylene, and C₄₊ olefins, particularly butylenes) manufactured according to the invention. The olefins manufactured according to the invention can also be used to synthesize such compounds as aldehydes, acids such as C₂-C₁₃ mono carboxylic acids, alcohols such as C₂-C₁₂ mono alcohols, esters that can be made from the C₂-C₁₂ mono carboxylic acids and the C₂-C₁₂ mono alcohols, linear alpha-olefins, vinyl acetate, ethylene dichloride and vinyl chloride, ethylbenzene, ethylene oxide, cumene, acrolein, allyl chloride, propylene oxide, acrylic acid, ethylene-propylene rubbers, acrylonitrile, trimers and dimers of ethylene and propylene, and the like, and blends and copolymers and combinations thereof. The C₄₊ olefins, butylene in particular, are particularly suited for the manufacture of aldehydes, acids, alcohols, esters that can be made from C₅-C₁₃ mono carboxylic acids and C₅-C₁₃ mono alcohols, and linear alpha-olefins.

F. EXAMPLES

The present invention can be better understood in view of the following non-limiting examples, which should not be read in any way to unduly limit the scope of the invention, as defined by the appended claims.

Example 1 OTO Conversion of a Methanol/Ethanol Feed Using SAPO+Yttria

In Example 1, the oxygenates-to-olefins process used a methanol feed with varying amounts of ethanol over a particulate SAPO molecular sieve catalyst, which is a CHA/AEI intergrowth (EMM-2) and having an Si:Al₂ ratio of about 0.1, and separate particles of yttrium oxide as the Group 3 metal oxide co-catalyst. The relative proportion of molecular sieve catalyst to metal oxide in Example 1 was about 5:1. The presence of ethanol in the methanol feed can typically lead to elevated levels of acetaldehyde in the product, e.g., through dehydrogenation of the ethanol. Process conditions of about 475° C. reactor temperature and about 25 psig (0.17 MPag) reactor pressure were used, as well as a WHSV of about 100 hr⁻¹, based on methanol. Prime olefin selectivity and prime olefin ratio results were obtained under these conditions and are shown in Table 1 below, along with the content of acetaldehyde impurity in the resultant product.

TABLE 1 Acetaldehyde % POS [wt %] POR formed [wt %] Ethanol EMM-2 + EMM-2 + EMM-2 + in Feed EMM-2 Y₂O₃ EMM-2 Y₂O₃ EMM-2 Y₂O₃  0 74.7 71.1 0.88 0.69 0.25 0.02 10 74.6 76.6 1.2 1.0 3.3 0.84 20 74.2 78.2 1.5 1.4 4.6 1.0

Table 1 indicates that POS did not change much with increasing ethanol content in the feedstock where there is no metal oxide co-catalyst. However, the use of a metal oxide co-catalyst in combination with the SAPO catalyst led to a significant increase in POS with increasing ethanol feed content.

Table 1 also indicates that POR increased steadily with increasing ethanol content in the feedstock, whether the metal oxide co-catalyst is present or not. In Example 1, the presence of metal oxide co-catalyst yielded reduced POR values compared to those of the SAPO catalyst alone.

Table 1 further indicates that the presence of ethanol in the feedstock significantly increases the acetaldehyde content in the product, but formation of this impurity can be significantly controlled through co-use of the metal oxide co-catalyst.

Example 2 OTO Conversion of a Methanol/Ethanol Feed According to the Invention Using an Aluminosilicate and a Basic Metal Oxide

In Example 2, the oxygenates-to-olefins process used a methanol feed with varying amounts of ethanol over a particulate aluminosilicate molecular sieve intergrowth catalyst having an Si:Al ratio of about 100 (high-silica) and separate particles of yttrium oxide as the Group 3 metal oxide co-catalyst. The relative proportion of molecular sieve catalyst to metal oxide in Example 2 was also about 5:1. As in Example 1, the presence of ethanol in the methanol feed can lead to elevated levels of acetaldehyde in the product, e.g., through dehydrogenation of the ethanol. Process conditions of about 540° C. reactor temperature and about 25 psig (0.17 MPag) reactor pressure were used, as well as a WHSV of about 100 hr⁻¹, based on methanol. Prime olefin selectivity and prime olefin ratio results were obtained under these conditions and are shown in Table 2 below, along with the content of acetaldehyde impurity in the resultant product.

TABLE 2 POS [wt %] POR Acetaldehyde Hi-Si Hi-Si formed [wt %] % Ethanol Hi-Si  cat + Hi-Si  cat + Hi-Si Hi-Si in Feed cat Y₂O₃ cat Y₂O₃ cat cat + Y₂O₃  0 76.0 73.9 1.2 1.2 0.16 <0.01 10 76.0 80.5 1.5 1.6 3.2 0.01 20 77.2 81.3 1.9 1.9 5.1 0.05

Table 2 indicates that the use of a metal oxide co-catalyst in combination with the high-silica aluminosilicate catalyst led to a significant increase in POS with increasing ethanol feed content. Indeed, at ethanol levels about 10 wt % or more in the feed, the product stream yielded a POS above about 80 wt %. Comparing this with the results shown in Table 1 with basic metal oxide co-catalyst included, the high-silica aluminosilicate catalyst showed at least about a 3 wt % improvement in POS over the SAPO at about 10-20% ethanol in the feedstock.

Table 2 also indicates that POR increased steadily with increasing ethanol content in the feedstock, whether the metal oxide co-catalyst is present or not. In Example 2, even at moderate ethanol content in the feedstock, the high-silica aluminosilicate catalyst system yielded much higher POR values, in contrast to the comparable SAPO catalyst system in Example 1. Furthermore, with the high-silica aluminosilicate catalyst, the presence of the basic metal oxide co-catalyst with mixed alcohol feeds did not show the same slight POR debit as in the comparable SAPO catalyst case from Example 1; instead, particularly at 20% ethanol in the feedstock, the aluminosilicate-yttria combination showed a slight POR advantage over the aluminosilicate catalyst alone. In many cases, although not in every case, it can be desirable to have a high POR, as ethylene monomer can tend to have a higher market value than propylene monomer.

Table 2 further indicates that there is almost no detectable acetaldehyde content in the aluminosilicate-yttria combination catalyst system, regardless of the ethanol feed content, which indicates a preferential dehydration of ethanol to ethylene in the aluminosilicate-yttria combination catalyst system, as opposed to the dehydrogenation reaction present in other variations in Examples 1-2. Thus, the co-use of the metal oxide co-catalyst with the high-silica aluminosilicate catalyst can significantly control formation of impurities such as acetaldehyde in the olefin product.

While the present invention has been described and illustrated by reference to particular embodiments, those of ordinary skill in the art will appreciate that the invention lends itself to variations not necessarily illustrated herein. For this reason, then, reference should be made solely to the appended claims for purposes of determining the true scope of the present invention. 

1. A process for converting an oxygenate feed to a light olefin product comprising: a) providing the oxygenate feed comprising a majority of methanol and at least about 5 wt % ethanol; b) providing a catalyst composition comprising an aluminosilicate catalyst and a basic metal oxide co-catalyst, wherein the aluminosilicate catalyst has an Si:Al ratio of at least about 50:1; and c) contacting the oxygenate feed with the catalyst composition under conditions sufficient to convert at least a portion of the oxygenate feed to a light olefin product.
 2. The process of claim 1, wherein the Si:Al ratio of the aluminosilicate catalyst is at least about 150:1.
 3. The process of claim 1, wherein the aluminosilicate catalyst comprises a molecular sieve having a structure comprising CHA, AEI, an intergrowth thereof, or a combination thereof.
 4. The process of claim 1, wherein the aluminosilicate catalyst comprises zeolite beta, ZSM-5, ZSM-11, ZSM-12, ZSM-20, ZSM-22, ZSM-23, ZSM-34, ZSM-35, ZSM-38, ZSM-48, ZSM-50, ZSM-58, MCM-1, MCM-2, MCM-3, MCM-4, MCM-5, MCM-9, MCM-10, MCM-14, MCM-22, MCM-41, M-41S, MCM-48, MCM-49, MCM-56, ultrastable Y zeolite (USY), mordenite, SSZ-13, ECR-18, an intergrowth thereof, or a combination thereof.
 5. The process of claim 1, wherein the basic metal oxide co-catalyst absorbs more than 0.03 mg of CO₂ per square meter of co-catalyst surface area at about 100° C.
 6. The process of claim 5, wherein the basic metal oxide co-catalyst absorbs more than 0.035 mg of CO₂ per square meter of co-catalyst surface area at about 100° C.
 7. The process of claim 1, wherein the basic metal oxide co-catalyst absorbs less than 5 mg of CO₂ per square meter of metal oxide surface area at about 100° C.
 8. The process of claim 1, wherein the basic metal oxide co-catalyst comprises a Group 2 metal oxide, a Group 4 metal oxide, hydrotalcite, or a combination thereof.
 9. The process of claim 1, wherein the basic metal oxide co-catalyst comprises yttria.
 10. The process of claim 1, wherein the ratio of aluminosilicate catalyst to basic metal oxide co-catalyst is from about 3:2 to about 15:1.
 11. The process of claim 1, wherein the oxygenate feed comprises at least about 60 wt % methanol and at least about 10 wt % ethanol.
 12. The process of claim 1, wherein the olefin product has (i) a prime olefin ratio of at least 1.5:1, (ii) a prime olefin selectivity of at least 80%, or (iii) both (i) and (ii).
 13. The process of claim 12, wherein the olefin product has (i) a prime olefin ratio of at least about 1.8:1, (ii) a prime olefin selectivity of at least about 81%, or (iii) both (i) and (ii).
 14. The process of claim 1, wherein the olefin product has an aldehyde content of not more than about 5,000 wppm.
 15. The process of claim 14, wherein the olefin product has an aldehyde content of not more than about 1,500 wppm.
 16. The process of claim 1, wherein the catalyst composition is contacted with the oxygenate feed at a temperature from about 450° C. to about 580° C.
 17. A process for converting an oxygenate feed to an olefin product comprising a) providing the oxygenate feed; b) providing a catalyst composition comprising an aluminosilicate catalyst and a basic metal oxide co-catalyst; and c) contacting the oxygenate feed with the catalyst composition under conditions sufficient to convert at least a portion of the oxygenate feed to a light olefin product having i) a prime olefin ratio of at least 1.5:1, ii) a prime olefin selectivity of at least 80%, or iii) both (i) and (ii).
 18. The process of claim 17, wherein the aluminosilicate catalyst has an Si:Al ratio of at least about 50:1.
 19. The process of claim 17, wherein the oxygenate feed comprises a majority of methanol and at least about 5 wt % ethanol.
 20. The process of claim 17, wherein the olefin product has an aldehyde content of not more than about 5,000 wppm.
 21. The process of claim 17, wherein the basic metal oxide co-catalyst absorbs more than 0.03 mg of CO₂ per square meter of co-catalyst surface area at about 100° C.
 22. A process for converting an oxygenate feed to an olefin product comprising: a) providing the oxygenate feed comprising a majority of methanol and at least about 5 wt % ethanol; b) providing a catalyst composition comprising an aluminosilicate catalyst; and c) contacting the oxygenate feed with the catalyst composition under conditions sufficient to convert at least a portion of the oxygenate feed to a light olefin product having an aldehyde content of not more than about 3,000 wppm.
 23. The process of claim 22, wherein the aluminosilicate catalyst has an Si:Al ratio of at least about 50:1.
 24. The process of claim 22, wherein the olefin product has (i) a prime olefin ratio of at least 1.5:1, (ii) a prime olefin selectivity of at least 80%, or (iii) both (i) and (ii).
 25. The process of claim 22, wherein catalyst composition further comprises a basic metal oxide co-catalyst that absorbs more than 0.03 mg of CO₂ per square meter of co-catalyst surface area at about 100° C. 